Preparation of fluorinated olefins via catalytic dehydrohalogenation of halogenated hydrocarbons

ABSTRACT

A process for making a fluorinated olefin having the step of dehydrochlorinating a hydrochlorofluorocarbon having at least one hydrogen atom and at least one chlorine atom on adjacent carbon atoms, preferably carried out in the presence of a catalyst selected from the group consisting of (i) one or more metal halides, (ii) one or more halogenated metal oxides, (iii) one or more zero-valent metals/metal alloys, (iv) a combination of two or more of the foregoing.

CROSS REFERENCE TO RELATED APPLICATIONS

This application is a division of U.S. application Ser. No. 12/167,159,filed Jul. 2, 2008 (now U.S. Pat. No. 9,040,759, issued May 26, 2015),which application claims priority to, and incorporates by reference,U.S. Provisional Application No. 60/958,468, filed Jul. 6, 2007.

BACKGROUND OF THE INVENTION 1. Field of the Invention

The present invention relates to the dehydrohalogenation of ahalogen-containing compound. The present invention further relates tothe dehydrochlorination of a hydrochlorofluorocarbon to a fluorinatedolefin.

2. Description of the Related Art

Chlorine-containing compounds, such as chlorofluorocarbons (CFCs), havebeen employed as refrigerants, foam blowing agents, cleaning agents,solvents, heat transfer media, sterilants, aerosol propellants,dielectrics, fire extinguishing agents, and power cycle working fluids.However, CFCs have proven to be detrimental to the Earth's ozone layer.Conventional substitutes for CFCs include hydrofluorocarbons (HFCs);however, these compounds have been found to contribute to globalwarming. For these reasons, there is a worldwide effort to develop newcompounds that are environmentally benign.

Partly or fully fluorinated olefins, including hydrofluoroolefins,(collectively referred to hereinafter as fluorinated olefins) arepotential replacements for HFCs and CFCs. They can be used in some ofthe aforementioned applications and can also be used as feedstockmonomers to synthesize fluoropolymers and other macromolecularcompounds.

Various methods for producing certain fluorinated olefins are known,including those involving the dehydrochlorination ofhydrochlorofluorocarbons. For example, U.S. patent application Ser. No.11/619,592 discloses a method for preparing 2,3,3,3-tetrafluoropropene(1234yf) via dehydrochlorination of 1,1,1,2-tetrafluoro-2-chloropropane(244bb) with the aid of a catalyst. The 244bb reactant can be preparedthrough liquid phase or gas phase catalytic fluorination of1,1,1-trifluoro-2-chloropropene (1233xf) with HF and 1233xf, in turn,can be made via gas phase fluorination of CCl₂═CClCH₂Cl(1,1,2,3-tetrachloropropene) with HF. The '592 application also teachesthe use of a carbon- and/or metal-based catalyst for the conversion of244bb to 1234yf. Depending on the reaction conditions, the conversion of244bb could be as high as 98%, but has a selectivity for 1234yf of only69% to 86%. Thus, there remains a need to develop a commercially viablecatalyst that not only is active, but also is more selective for 1234yf.

However, the conversion of a hydrochlorofluorocarbon to a fluorinatedolefin by conventional methods is problematic because by-products oftenform and undergo a competing dehydrofluorination reaction. Hence, itwould be advantageous to develop a catalyst system that can suppressundesirable dehydrofluorination reactions, so that single-passproductivity and yield of the desired fluorinated olefin can beincreased.

SUMMARY OF THE INVENTION

According to the present invention, provided a process for making afluorinated olefin via dehydrochlorination of a hydrochlorofluorocarbonhaving at least one hydrogen atom and at least one chlorine atom onadjacent carbon atoms. The dehydrochlorination is carried out in thepresence of a catalyst selected from the group consisting of (i) one ormore metal halides, (ii) one or more halogenated metal oxides, (iii) oneor more zero-valent metals/metal alloys, and (iv) a combination of twoor more of the foregoing. Preferred fluorinated olefin products are thefollowing: 2,3,3,3-tetrafluoropropene (1234yf),1,3,3,3-tetrafluoropropene (trans/cis-1234ze),1,2,3,3,3-pentafluoropropene (Z/E-1255ye), 1,1,3,3,3-pentafluoropropene(1225zc), and 1,1,2,3,3,3-hexafluoropropene (1216).

DETAILED DESCRIPTION OF THE INVENTION

In the present invention, a hydrochlorofluorocarbon having at least onehydrogen and at least one chlorine on adjacent carbons isdehydrochlorinated in the presence of a catalyst to form a producthaving a fluorinated olefin therein. Table 1 sets forth examples offluorinated olefins and precursor hydrochlorofluorocarbons from whichthey can be obtained (i.e., hydrochlorofluorocarbon in left column andcorresponding fluorinated olefin in the right column).

TABLE 1 Hydrochlorofluorocarbon Fluorinated olefin(s)chlorotetrafluoropropane tetrafluoropropene chloropentafluoropropanepentafluoropropene chlorohexafluoropropane hexafluoropropene1,1,1,2-tetrafluoro-2-chloropropane 2,3,3,3-tetrafluoropropeneCF₃CFClCH₃ (244bb) CF₃CF═CH₂ (1234yf)1,1,1,2-tetrafluoro-3-chloropropane 2,3,3,3-tetrafluoropropeneCF₃CHFCH₂Cl (244eb) CF₃CF═CH₂ (1234yf)1,1,1,3-tetrafluoro-3-chloropropane 1,3,3,3-tetrafluoropropeneCF₃CH₂CHFCl (244fa) CF₃CH═CHF (trans/cis-1234ze)1,1,1,3-tetrafluoro-2-chloropropane 1,3,3,3-tetrafluoropropeneCF₃CHClCH₂F (244db) CF₃CH═CHF (trans/cis-1234ze)1,1,1,2,3-pentafluoro-2-chloropropane 1,2,3,3,3-pentafluoropropeneCF₃CFClCH₂F (235bb) CF₃CF═CHF (Z/E-1225ye)1,1,1,2,3-pentafluoro-3-chloropropane 1,2,3,3,3-pentafluoropropeneCF₃CHFCHFCl (235ea) CF₃CF═CHF (Z/E-1225ye)1,1,1,3,3-pentafluoro-3-chloropropane 1,1,3,3,3-pentafluoropropeneCF₃CH₂CF₂Cl (235fa) CF₃CH═CF₂ (1225zc)1,1,1,3,3-pentafluoro-2-chloropropane 1,1,3,3,3-pentafluoropropeneCF₃CHClCHF₂ (235da) CF₃CH═CF₂ (1225zc)1,1,1,2,3,3-hexafluoro-2-chloropropane 1,1,2,3,3,3-hexafluoropropeneCF₃CFClCHF₂ (226ba) CF₃CF═CF₂ (1216)1,1,1,2,3,3-hexafluoro-3-chloropropane 1,1,2,3,3,3-hexafluoropropeneCF₃CHFCF₂Cl (226ea) CF₃CF═CF₂ (1216)

In the process of the present invention, selected catalysts are employedto enhance the selectivity and/or conversion of hydrochlorofluorocarbonsto fluorinated olefins. The catalysts are more selective for thedehydrochlorination reaction, which produces fluorinated olefin, thanfor the competing dehydrofluorination side reaction, which produces theundesirable byproduct chlorine-containing olefin.

There are three preferred classes of catalysts useful in the presentinvention: (i) metal halides, (ii) halogenated metal oxides, and (iii)zero-valent metals/metal alloys.

The first class of catalysts is metal halides, preferably mono-, bi-,and tri-valent metal halides and their mixtures/combinations, and morepreferably mono- and bi-valent metal halides and theirmixtures/combinations. Component metals include, but are not limited to,Cr³⁺, Fe³⁺, Mg²⁺, Ca²⁺, Ni²⁺, Zn²⁺, Pd²⁺, Li⁺, Na⁺, K⁺, and Cs⁺.Component halogens include, but are not limited to, F⁻, Cl⁻, Br⁻, andI⁻. Examples of useful mono- or bi-valent metal halide include, but arenot limited to, LiF, NaF, KF, CsF, MgF₂, CaF₂, LiCl, NaCl, KCl, andCsCl. The catalyst may be supported or unsupported. A preferred catalystis a CsCl/MgF₂ combination. A particularly preferred catalyst is aCsCl/MgF₂ combination wherein CsCl is present in an amount of about 5.0to about 50 wt % based on the total weight of the catalyst.

The second class of catalysts is halogenated metal oxides, preferablyhalogenated mono-, bi-, and tri-valent metal oxides and theirmixtures/combinations, and more preferably halogenated mono- andbi-valent metal oxides and their mixtures/combinations. Component metalsinclude, but are not limited to, Cr³⁺, Fe³⁺, Mg²⁺, Ca²⁺, Ni²⁺, Zn²⁺,Pd²⁺, Li⁺, Na⁺, K⁺, and Cs⁺. Halogenation treatments can include any ofthose known in the prior art, particularly those that employ HF, F₂,HCl, Cl₂, HBr, Br₂, HI, and I₂ as the halogenation source. Examples ofuseful halogenated mono- and bi-valent metal oxides include, but are notlimited to, fluorinated or chlorinated MgO, fluorinated or chlorinatedCaO, fluorinated or chlorinated Li₂O, fluorinated or chlorinated Na₂O,fluorinated or chlorinated K₂O, and fluorinated or chlorinated Cs₂O. Thecatalyst may be supported or unsupported.

The third class of catalysts is neutral (i.e., zero valent) metals,metal alloys, and their mixtures. Useful metals include, but are notlimited to, Pd, Pt, Rh, Fe, Co, Ni, Cu, Mo, Cr, Mn, and combinations ofthe foregoing as alloys or mixtures. The catalyst may be supported orunsupported. Useful examples of metal alloys include, but are notlimited to, SS 316, Monel 400, Inconel 825, Inconel 600, and Inconel625.

In addition to the fluorinated olefin, i.e., the hydrofluorocarbon orfluorocarbon, the product mixture may also have unconvertedhydrochlorofluorocarbon and hydrogen chloride.

Enhanced or improved selectivity for the target product is an importantfeature of the present invention. The dehydrochlorination reaction ispreferably carried out at a selectivity of at least about 50%, morepreferably at least about 70%, and most preferably at least about 80%.Conversion is preferably about 25% or more and most preferably about 40%or more.

Dehydrochlorination may be carried out at a temperature range of about200° C. to about 800° C., preferably from about 300° C. to about 600°C., and more preferably from about 400° C. to about 500° C. in thepresence of a catalyst. It is contemplated that a variety of reactionpressures may be used, such as superatmospheric, atmospheric, andsubatmospheric. Atmospheric pressure is preferred.

Dehydrochlorination may optionally be carried out in presence or absenceof an oxidizing agent. Useful examples of oxidizing agents include, butare not limited to, oxygen and carbon dioxide. Use of an oxidizing agentcan extend the life of the catalyst. The oxidizing agent can be pure ordiluted with an inert gas such as nitrogen before being introduced intoreactor. The level of oxidizing agent is generally from about 1% toabout 10% by volume and preferably from about 2% to 5% by volume basedon the volume of the organic feed.

It may also be advantageous to periodically regenerate the catalystafter prolonged use while in place in the reactor. Regeneration of thecatalyst may be accomplished by any means known in the art. One methodis by passing oxygen or oxygen diluted with nitrogen over the catalystat temperatures of about 200° C. to about 600° C. (preferably about 350°C. to about 450° C.) for about 0.5 hour to about 3 days followed byeither halogenation treatment at temperatures of about 25° C. to about400° C. (preferably about 200° C. to about 350° C.) for halogenatedmetal oxide catalysts and metal halide ones or reduction treatment attemperatures of about 100° C. to about 600° C. (preferably about 200° C.to about 350° C.) for metal catalysts.

Dehydrochlorination is preferably carried out in a corrosion-resistantreaction vessel. Examples of corrosion-resistant materials areHastelloy, Inconel, Monel and fluoropolymer linings. The vessel may havea fixed or a fluidized catalyst bed. If desired, inert gases such asnitrogen or argon may be employed in the reactor during operation.

EXAMPLES

The following are examples of the present invention and are not to beconstrued as limiting.

Example 1: 244bb Dehydrohalogenation Over Metal Fluoride and FluorinatedMetal Oxide Catalysts

A series of mono-, bi-, and tri-valent metal fluorides and fluorinatedbi- and tri-valent metal oxides were used as dehydrohalogenationcatalysts. Approximately 20 cc of catalyst pellets was used in a typicalrun. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf waspassed through the catalyst bed at a rate of 6 g/h at a temperature thatranged from 200° C. to 600° C. The temperatures at the bottom ofcatalyst bed and at the top of catalyst bed were measured.

As shown in Table 2, NaF, MgF₂, CaF₂, and fluorinated MgO were able toprovide a selectivity to 1234yf higher than 80%, while FeF₃ andfluorinated Cr₂O₃ exhibited a selectivity to 1233xf higher than 80%.Selectivity is based on mole percent. These results indicate that mono-and bi-valent metal halides as well as halogenated mono- and bi-valentmetal oxides are more favorable than their trivalent counterparts ascatalysts for 244bb dehydrochlorination. Among NaF, MgF₂, CaF₂, andfluorinated MgO, MgF₂ exhibited the best performance; it provided aconversion of 244bb above 50% and a selectivity to 1234yf above 85%after 8 h (hours) on stream.

TABLE 2 (Dehydrohalogenation of 244bb over various mono-, bi-, andtri-valent metal fluorides and fluorinated bi- and tri-valent metaloxides*) Temp. Con- Bottom- version Selectivity Selectivity SelectivityTop t 244bb 1234yf 1233xf Unknowns Catalyst (° C.) (h) (%) (%) (%) (%)NaF 450-554 1 24.8 92.2 7.8 450-553 2 22.3 90.3 9.7 450-553 3 19.6 89.610.4 450-553 4 15.6 89.1 10.9 450-553 5 12.6 87.4 12.6 fluorinated450-517 1 25.3 94.6 5.4 MgO 450-517 2 26.5 96.0 4.0 450-518 3 25.8 96.83.2 450-518 4 25.4 97.1 2.9 450-516 5 26.6 97.3 2.7 450-516 6 26.3 97.52.5 MgF₂ 475-506 1 48.2 76.9 17.7 5.4 475-509 2 52.9 79.8 14.6 5.6475-509 3 53.3 80.7 12.9 6.4 475-507 4 52.4 81.4 11.9 6.7 475-509 5 54.283.0 10.9 6.1 475-510 6 54.1 83.6 10.2 6.2 475-508 7 54.7 84.7 9.6 5.7475-509 8 53.7 85.4 9.2 5.4 475-510 9 54.9 86.0 8.6 5.5 475-509 10 53.586.7 8.2 5.1 CaF₂ 450-511 1 7.0 76.8 23.2 450-510 2 7.3 80.2 19.8Fluorinated 250-317 1 95.3 6.2 92.6 1.2 Cr₂O₃ 250-316 2 55.0 8.0 89.22.8 FeF₃ 350-385 1 90.4 10.9 88.7 0.4 350-385 2 84.7 11.0 88.5 0.5*Reaction conditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0%1233xf, 1 atm

Example 2: 244bb Dehydrohalogenation Over Alkaline Metal Chloride-DopedMgF₂ Catalysts

A series of alkaline metal chlorides were investigated as an additive toMgF₂ with a purpose of improving the selectivity to 1234yf. Forcomparison purpose, the results obtained over MgF₂ catalyst were alsoreported. Approximately 20 cc of catalyst pellets was used in a typicalrun. A mixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf waspassed through catalyst bed at a rate of 6 g/h (grams/hour) at atemperature that ranged from 470° C. to 520° C. The temperatures at thebottom of catalyst bed and at the top of catalyst bed were measured.

As shown in Table 3, the MgF₂ provided a 244bb conversion of 53-55%, a1234yf selectivity of 80-87%, and a 1233xf selectivity of 8-15%; the 10%LiCl/MgF₂ provided a 244bb conversion below 45%, a 1234yf selectivity ofabout 90%, and a 1233xf selectivity of about 5%; the 10% KCl/MgF₂provided a 244bb conversion below 50%, a 1234yf selectivity of about96%, and a 1233xf selectivity of about 1%; and the 10% CsCl/MgF₂provided a 244bb conversion of 50-52%, a 1234yf selectivity of about97%, and essentially no formation of 1233xf. CsCl exhibited the bestresults, while the 10% CsCl/MgF₂ catalyst provided activity comparableto MgF₂ and the highest 1234yf selectivity while generating no 1233xf.

TABLE 3 (Reactivity of MgF₂ and alkaline metal chloride-doped MgF₂catalysts during 244bb dehydrohalogenation*) Temp. Con- Select- Bottom-version Selectivity ivity Selectivity, Top t 244bb 1234yf 1233xfUnknowns Catalyst (°) (h) (%) (%) (%) (%) MgF₂ 475-506 1 48.2 76.9 17.75.4 475-509 2 52.9 79.8 14.6 5.6 475-509 3 53.3 80.7 12.9 6.4 475-507 452.4 81.4 11.9 6.7 475-509 5 54.2 83.0 10.9 6.1 475-510 6 54.1 83.6 10.26.2 475-508 7 54.7 84.7 9.6 5.7 475-509 8 53.7 85.4 9.2 5.4 475-510 954.9 86.0 8.6 5.5 475-509 10 53.5 86.7 8.2 5.1 10 wt % 475-490 1 29.489.1 5.3 5.6 LiCl/MgF₂ 475-506 2 38.8 89.6 5.3 5.0 475-505 3 40.4 89.95.2 4.9 475-507 4 42.9 90.5 4.8 4.7 10 wt % 475-514 1 38.3 95.1 0.9 4.0KCl/MgF₂ 475-515 3 47.2 95.6 0.8 3.6 475-515 5 47.5 95.8 0.7 3.5 475-5096 43.7 95.8 0.6 3.5 475-514 7 47.1 95.8 0.7 3.5 10 wt % 475-511 1 49.696.9 3.1 CsCl/MgF₂ 475-510 2 51.2 97.0 3.0 475-511 3 51.8 96.9 3.1475-508 4 50.4 96.9 3.1 475-510 5 51.4 97.0 3.0 *Reaction conditions: 20ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 3: 244bb Dehydrohalogenation Over CsCl/MgF₂ Catalysts

A series of CsCl/MgF₂ catalysts with different loadings of CsCl wereinvestigated with a purpose of optimizing CsCl loading. 20 cc ofcatalyst pellets was used in a typical run. A mixture containing 97.2wt. % 244bb and 2.0 wt. % 1233xf was passed through the catalyst bed ata rate of 6 g/h at a temperature that ranged from 470° C. to 520° C. Thetemperatures at the top and bottom of the catalyst bed were measured. Asshown in Table 4, the selectivity to 1233xf decreased with increasingCsCl loading from 0.0 to 5.0 wt %, and no 1233xf was formed overcatalysts with CsCl loadings ≥7.5 wt % based on the total weight of thecatalyst.

TABLE 4 (Effect of CsCl loading on the performance of CsCl/MgF₂catalysts during 244bb dehydrohalogenation*) Temp. CsCl Bottom-Conversion Selectivity Selectivity Selectivity loading Top t 244b 1234yf1233xf Unknowns (wt. %) (°) (h) (%) (%) (%) (%) 0.0 475-506 1 48.2 76.917.7 5.4 475-509 2 52.9 79.8 14.6 5.6 475-509 3 53.3 80.7 12.9 6.4475-507 4 52.4 81.4 11.9 6.7 475-509 5 54.2 83.0 10.9 6.1 475-510 6 54.183.6 10.2 6.2 475-508 7 54.7 84.7 9.6 5.7 475-509 8 53.7 85.4 9.2 5.4475-510 9 54.9 86.0 8.6 5.5 475-509 10 53.5 86.7 8.2 5.1 2.5 500-514 148.4 88.7 5.2 6.1 500-514 2 48.1 88.5 5.2 6.3 500-514 3 49.5 89.1 5.05.9 500-507 4 46.9 89.3 4.8 5.9 500-509 5 48.5 89.9 4.6 5.5 500-513 648.5 89.6 4.7 5.7 500-514 7 49.6 89.9 4.6 5.5 5.0 490-510 1 49.0 94.80.5 4.7 490-511 2 51.0 94.5 0.4 5.1 490-510 3 49.2 95.3 0.5 4.2 490-5054 48.7 95.0 0.4 4.6 490-507 6 49.8 95.4 0.4 4.2 490-503 8 49.2 95.7 0.43.9 7.5 475-510 2 41.9 94.6 5.4 475-507 3 41.6 95.8 4.2 475-508 4 46.196.5 3.5 475-506 7 43.5 96.5 3.5 475-506 8 42.2 96.4 3.6 475-507 9 44.096.6 3.4 10.0 475-511 1 49.6 96.9 3.1 475-510 2 51.2 97.0 3.0 475-511 351.8 96.9 3.1 475-508 4 50.4 96.9 3.1 475-510 5 51.4 97.0 3.0 *Reactionconditions: 20 ml of catalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1atm

Example 4: 244bb Dehydrohalogenation Over Non-Precious Metal-Doped MgF₂Catalysts

A series of non-precious metals were investigated as additives to MgF₂with a purpose of improving the selectivity to 1234yf. For comparisonpurposes, the results obtained over MgF₂ catalyst were also reported.Approximately 20 cc of catalyst pellets was used in a typical run. Amixture containing 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passedthrough catalyst bed at a rate of 6 g/h at a temperature that rangedfrom 440 to 540° C. The temperatures at the top and bottom of thecatalyst bed were measured.

As shown in Table 5, the addition of cobalt and especially nickelresulted in the decrease in the selectivity to 1233xf, while theaddition of iron resulted in an increase in the selectivity to 1233xf.The 12 wt % Ni/MgF₂ catalyst provided a 1234yf selectivity of about 95%with a 1233xf selectivity of about 2%.

TABLE 5 (Reactivity of MgF₂ and metal-doped MgF₂ catalysts during 244bbdehydrohalogenation*) Temp. Con- Bottom- version Selectivity SelectivitySelectivity, Top t 244bb 1234yf 1233xf Unknowns Catalyst (°) (h) (%) (%)(%) (%) MgF₂ 450-529 1 53.5 69.0 26.0 5.0 450-529 2 58.9 74.7 20.8 4.5450-528 3 60.4 77.9 17.4 4.7 450-530 4 64.5 81.0 14.3 4.7 450-529 5 61.482.4 12.9 4.8 450-528 6 62.3 84.3 10.8 4.8 450-529 7 63.7 85.3 9.7 5.0450-527 8 66.8 86.6 8.6 4.7 450-526 9 64.3 87.0 8.2 4.8 450-530 10 63.587.8 7.6 4.5 450-528 11 63.8 88.2 7.2 4.6 450-530 12 64.7 88.3 6.8 4.8450-528 13 64.1 88.6 6.6 4.8 450-528 14 63.2 89.3 6.2 4.5 12 wt %450-525 1 71.2 53.4 41.7 4.9 Fe/MgF₂ 450-523 2 72.8 53.0 41.9 5.1 12 wt% 445-527 2 48.5 88.8 7.9 4.3 Co/MgF₂ 445-528 3 58.0 90.1 6.7 3.2445-528 4 62.8 90.9 5.9 3.2 445-527 5 66.6 91.5 5.2 3.3 12 wt % 445-5267 54.7 93.0 2.0 5.0 Ni/MgF₂ 445-527 8 53.2 93.4 2.1 4.5 445-526 10 56.294.8 2.0 3.2 445-526 11 58.6 94.5 2.0 3.4 *Reaction conditions: 20 ml ofcatalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

Example 5: 244bb Dehydrohalogenation Over Metal and Metal AlloyCatalysts

A series of supported and unsupported metals as well as metal alloyswere used as dehydrohalogenation catalysts. 20 cc of catalyst pellets ora 4 inch-long metal mesh roll was used in a typical run. A mixturecontaining 97.2 wt. % 244bb and 2.0 wt. % 1233xf was passed through acatalyst bed at a rate of 6 g/h at a temperature ranged from 420° C. to480° C. The temperatures at the top and bottom of the catalyst bed weremeasured. As shown in Table 6, all the metal and metal alloy catalystswere active and extremely selective for 244bb dehydrochlorination(1234yf selectivity >95%) while generating no 1233xf. Compared to metalhalide and/or halogenated metal oxide catalysts, the metal catalysts didnot require as high an operating temperature.

TABLE 6 (reactivity of metal and metal alloys during 244bbdehydrohalogenation*) Temp. Con- Bottom- version Selectivity SelectivitySelectivity, Top t 244b 1234yf 1233xf Unknowns Catalyst (° C.) (h) (%)(%) (%) (%) 5 wt % 450-478 1 43.6 95.3 4.7 Pd/BaSO₄ 450-476 2 30.5 94.65.4 450-478 3 30.1 92.9 7.1 450-475 4 29.6 95.1 4.9 450-481 5 31.1 94.85.2 Ni mesh 425-473 1 45.8 96.9 3.1 425-473 2 45.5 97.3 2.7 425-473 344.8 97.8 2.2 425-473 4 43.7 97.9 2.1 425-473 5 42.1 97.9 2.1 425-473 640.5 98.0 2.0 425-472 7 39.5 98.0 2.0 425-473 8 38.6 98.0 2.0 425-473 938.6 98.9 1.1 425-474 10 39.2 98.1 1.9 Inconel 425-464 1 26.5 95.8 4.2600 chips 425-467 2 32.6 97.9 2.1 425-470 3 36.9 98.1 1.9 425-470 4 40.198.1 1.9 425-470 5 40.4 98.3 1.7 425-470 6 41.8 98.4 1.6 425-468 7 42.598.5 1.5 425-468 8 41.4 98.6 1.4 425-466 9 39.7 98.6 1.4 425-466 10 37.198.7 1.3 20cc 425-466 1 25.7 97.3 2.7 Inconel 425-467 2 28.8 97.6 2.4625 chips 425-467 4 33.4 97.9 2.1 425-459 6 33.8 98.0 2.0 425-465 8 36.298.1 1.9 425-463 10 36.8 98.1 1.9 425-465 12 38.0 98.2 1.8 425-465 1437.7 98.2 1.8 425-462 16 39.1 99.1 0.9 *Reaction conditions: 20 ml ofcatalyst, 6 g-organic/h, 97.2% 244bb/2.0% 1233xf, 1 atm

It should be understood that the foregoing description is onlyillustrative of the present invention. Various alternatives andmodifications can be devised by those skilled in the art withoutdeparting from the invention. Accordingly, the present invention isintended to embrace all such alternatives, modifications and variancesthat fall within the scope of the appended claims.

What is claimed is:
 1. A process for making a three carbon fluorinatedolefin, comprising: dehydrochlorinating a three carbonhydrochlorofluorocarbon having at least one hydrogen and at least onechlorine on adjacent carbons in the presence of a catalyst selected fromone or more zero-valent metal alloys, wherein the zero-valent metalalloy comprises Pd, Pt, Rh, Fe, Co, Ni, Mo, Cr, Mn, and combinations ofthese; and wherein the hydrochlorofluorocarbon and resulting fluorinatedolefin is selected from the group consisting of1,1,1,2-tetrafluoro-2-chloropropane and 2,3,3,3-tetrafluoropropene,1,1,1,2-tetrafluoro-3-chloropropane and 2,3,3,3-tetrafluoropropene,1,1,1,3-tetrafluoro-3-chloropropane and 1,3,3,3-tetrafluoropropene,1,1,1,3-tetrafluoro-2-chloropropane and 1,3,3,3-tetrafluoropropene,1,1,1,2,3-pentafluoro-2-chloropropane and 1,2,3,3,3-pentafluoropropene,1,1,1,2,3-pentafluoro-3-chloropropane and 1,2,3,3,3-pentafluoropropene,1,1,1,3,3-pentafluoro-3-chloropropane and 1,1,3,3,3-pentafluoropropene.2. The process of claim 1, wherein the hydrochlorofluorocarbon is1,1,1,2-tetrafluoro-2-chloropropane and the fluorinated olefin is2,3,3,3-tetrafluoropropene.
 3. The process of claim 1, wherein the oneor more zero-valent metal alloys is a Ni alloy.
 4. The process of claim1, wherein said zero valent metal alloy is selected from SS 316, Monel400, lnconel 825, lnconel 600 and lnconel
 625. 5. The process of claim1, wherein dehydrochlorination is carried out at a temperature of fromabout 300 to about 600° C.
 6. The process of claim 1, whereindehydrochlorination is carried out at a temperature of from about 400 toabout 500° C.
 7. The process of claim 6, wherein the catalyst comprisesNi.
 8. The process of claim 1, wherein the catalyst comprises Ni.
 9. Theprocess of claim 1, wherein the catalyst comprises lnconel
 600. 10. Theprocess of claim 9, wherein the catalyst comprises lnconel 600 chips.11. The process of claim 1, wherein said zero valent metal alloy isselected from lnconel 600 and lnconel
 625. 12. The process of claim 1,wherein said zero valent metal alloy is lnconel
 600. 13. The process ofclaim 1, wherein said zero valent metal alloy is lnconel
 625. 14. Aprocess for making a fluorinated olefin, comprising: dehydrochlorinatinga hydrochlorofluorocarbon having at least one hydrogen and at least onechlorine on adjacent carbons in the presence of catalyst comprising azero valent metal alloy selected from Inconel 625 and Inconel
 600. 15.The process of claim 14, wherein dehydrochlorination is carried out at atemperature of from about 300 to about 600° C.
 16. The process of claim14, wherein dehydrochlorination is carried out at a temperature of fromabout 400 to about 500° C.
 17. The process of claim 14, wherein saidzero valent metal alloy is lnconel
 600. 18. The process of claim 14,wherein said zero valent metal alloy is lnconel
 625. 19. The process ofclaim 14, wherein the hydrochlorofluorocarbon and resulting fluorinatedolefin is selected from the group consisting of1,1,1,2-tetrafluoro-2-chloropropane and 2,3,3,3-tetrafluoropropene,1,1,1,2-tetrafluoro-3-chloropropane and 2,3,3,3-tetrafluoropropene,1,1,1,3-tetrafluoro-3-chloropropane and 1,3,3,3-tetrafluoropropene,1,1,1,3-tetrafluoro-2-chloropropane and 1,3,3,3-tetrafluoropropene,1,1,1,2,3-pentafluoro-2-chloropropane and 1,2,3,3,3-pentafluoropropene,1,1,1,2,3-pentafluoro-3-chloropropane and 1,2,3,3,3-pentafluoropropene,1,1,1,3,3-pentafluoro-3-chloropropane and 1,1,3,3,3-pentafluoropropene.20. The process of claim 14, wherein the hydrochlorofluorocarbon is1,1,1,2-tetrafluoro-2-chloropropane and the fluorinated olefin is2,3,3,3-tetrafluoropropene.